EP0928842A2 - Feuchte Grobpartikel und Verfahren zur Herstellung der feuchten Grobpartikel - Google Patents

Feuchte Grobpartikel und Verfahren zur Herstellung der feuchten Grobpartikel Download PDF

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Publication number
EP0928842A2
EP0928842A2 EP19990106332 EP99106332A EP0928842A2 EP 0928842 A2 EP0928842 A2 EP 0928842A2 EP 19990106332 EP19990106332 EP 19990106332 EP 99106332 A EP99106332 A EP 99106332A EP 0928842 A2 EP0928842 A2 EP 0928842A2
Authority
EP
European Patent Office
Prior art keywords
cake
particles
path
weight
wet particles
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP19990106332
Other languages
English (en)
French (fr)
Other versions
EP0928842A3 (de
Inventor
Edward G. Knapick
Ernest P. Wolfer
Brent Willemsen
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Marcal Paper Mills LLC
Original Assignee
Marcal Paper Mills LLC
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Marcal Paper Mills LLC filed Critical Marcal Paper Mills LLC
Publication of EP0928842A2 publication Critical patent/EP0928842A2/de
Publication of EP0928842A3 publication Critical patent/EP0928842A3/de
Withdrawn legal-status Critical Current

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Classifications

    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21F—PAPER-MAKING MACHINES; METHODS OF PRODUCING PAPER THEREON
    • D21F1/00—Wet end of machines for making continuous webs of paper
    • D21F1/66—Pulp catching, de-watering, or recovering; Re-use of pulp-water
    • A—HUMAN NECESSITIES
    • A01—AGRICULTURE; FORESTRY; ANIMAL HUSBANDRY; HUNTING; TRAPPING; FISHING
    • A01K—ANIMAL HUSBANDRY; AVICULTURE; APICULTURE; PISCICULTURE; FISHING; REARING OR BREEDING ANIMALS, NOT OTHERWISE PROVIDED FOR; NEW BREEDS OF ANIMALS
    • A01K1/00—Housing animals; Equipment therefor
    • A01K1/015—Floor coverings, e.g. bedding-down sheets ; Stable floors
    • A01K1/0152—Litter
    • A01K1/0154—Litter comprising inorganic material
    • A—HUMAN NECESSITIES
    • A01—AGRICULTURE; FORESTRY; ANIMAL HUSBANDRY; HUNTING; TRAPPING; FISHING
    • A01K—ANIMAL HUSBANDRY; AVICULTURE; APICULTURE; PISCICULTURE; FISHING; REARING OR BREEDING ANIMALS, NOT OTHERWISE PROVIDED FOR; NEW BREEDS OF ANIMALS
    • A01K1/00—Housing animals; Equipment therefor
    • A01K1/015—Floor coverings, e.g. bedding-down sheets ; Stable floors
    • A01K1/0152—Litter
    • A01K1/0155—Litter comprising organic material
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05D—INORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C; FERTILISERS PRODUCING CARBON DIOXIDE
    • C05D3/00—Calcareous fertilisers
    • C05D3/02—Calcareous fertilisers from limestone, calcium carbonate, calcium hydrate, slaked lime, calcium oxide, waste calcium products
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05D—INORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C; FERTILISERS PRODUCING CARBON DIOXIDE
    • C05D9/00—Other inorganic fertilisers
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05G—MIXTURES OF FERTILISERS COVERED INDIVIDUALLY BY DIFFERENT SUBCLASSES OF CLASS C05; MIXTURES OF ONE OR MORE FERTILISERS WITH MATERIALS NOT HAVING A SPECIFIC FERTILISING ACTIVITY, e.g. PESTICIDES, SOIL-CONDITIONERS, WETTING AGENTS; FERTILISERS CHARACTERISED BY THEIR FORM
    • C05G3/00—Mixtures of one or more fertilisers with additives not having a specially fertilising activity
    • C05G3/80—Soil conditioners
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05G—MIXTURES OF FERTILISERS COVERED INDIVIDUALLY BY DIFFERENT SUBCLASSES OF CLASS C05; MIXTURES OF ONE OR MORE FERTILISERS WITH MATERIALS NOT HAVING A SPECIFIC FERTILISING ACTIVITY, e.g. PESTICIDES, SOIL-CONDITIONERS, WETTING AGENTS; FERTILISERS CHARACTERISED BY THEIR FORM
    • C05G5/00—Fertilisers characterised by their form
    • C05G5/40—Fertilisers incorporated into a matrix
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
    • D21B1/00—Fibrous raw materials or their mechanical treatment
    • D21B1/04—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres
    • D21B1/12—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres by wet methods, by the use of steam
    • D21B1/30—Defibrating by other means
    • D21B1/32—Defibrating by other means of waste paper
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
    • D21B1/00—Fibrous raw materials or their mechanical treatment
    • D21B1/38—Conserving the finely-divided cellulosic material
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies
    • Y02W30/64—Paper recycling

Definitions

  • the present invention relates to recycling wastepaper, and more particularly to recycling processes for recovering papermaking fibers and for making absorbent granular materials from wastepaper.
  • waste paper such as newspapers, magazines, office paper waste
  • the paper fibers are separated from the other solid components by using large quantities of water.
  • the printing materials such as laser print, photocopier print and ink, are removed before the paper fibers are conducted to the papermaking machine.
  • these rejected solid materials are discharged with the water into large settling basins.
  • the solid materials that settle out in the basins are then dumped in a landfill, or otherwise discarded.
  • the material that settles out in the basins is known as paper mill sludge.
  • the process of this invention utilizes wastepaper, preferably office waste that is printed with laser print, photocopier print, or other inks, as well as stationery and magazines that have a coated surface.
  • wastepaper is pulped with water, caustic and surfactants to produce a slurry containing cellulose fibers, cellulose fines and fillers.
  • the slurry passes through wire washers which separate papermaking fibers from the fines and fillers.
  • Papermaking fibers are a mixture of long and short fibers, although it is recognized that some of the short fibers will pass through the screens.
  • long fibers are greater than about 1 mm in length and short fibers are between about 1 mm and about 0.1 mm in length.
  • the papermaking fiber stream also referred to as the "accepts stream" is directed through a cleaning and deinking step and then to a conventional papermaking machine for processing into paper.
  • various streams from the papermaking machine and other sources are passed through a fiber recovery system where a series of wire washers separate papermaking fibers from these streams, sending the papermaking fibers back to the cleaning and deinking stages.
  • the rejects from this fiber recovery system contain essentially the same solid materials as the first reject stream mentioned above.
  • These reject streams are combined and sent to a flotation clarifier where a flocculating polymer is added and air is injected to cause the suspended solids (fines and fillers) to be concentrated as a flotate. Clarified water is removed from the clarifier for reuse in the process.
  • the flotate stream is pasteurized at a minimum temperature of 160 degrees F., and then a second flocculating polymer is added to the flotate stream.
  • This flotate stream then passes through a belt press or similar dewatering device where the water content is further reduced.
  • the filter cake from the belt press is in the form of a gray, wet cake.
  • the wet cake then passes to a size reducer where the material is broken up.
  • the wet granules are then sent through a conveyor dryer to produce dry granules of irregular shape and having good absorbent characteristics.
  • the granules produced by this process have a high liquid holding capacity.
  • the term granules is intended to include small particles and chunks that may be as large as 0.5 inches across.
  • Their composition, by weight is approximately 35-50% inorganic fillers (kaolin clay, calcium carbonate, titanium dioxide) and 50-65% organic (cellulose fines, starches, tannins, lignin, etc.). Less than 10% of the cellulosic material in the granules is in the form of fibers greater than 1 mm in length.
  • the granules are free flowing and resistant to attrition.
  • the bulk density of the granules is between 28-38 lbs./cu.ft. These granules are useful as oil and water absorbents as well as carriers for agricultural chemicals.
  • the process of this invention utilizes wastepaper that is collected from offices or other sources that contain primarily recyclable paper grades, including magazines (with clay and calcium carbonate based coatings) and printed paper such as paper used for laser printing, photocopying and other paper.
  • wastepaper is supplied to a hydropulper 2 along with water, caustic agents, such as sodium hydroxide, and dispersants to separate the fiber from the other components of the wastepaper. Plastics, debris and other foreign objects are removed by conventional means.
  • the pulp slurry from the hydropulper which contains more than 95% water, passes through a pipe 4 to a washer 6 where several conventional washing steps are performed.
  • the slurry flows over wire screens where fibers useful for papermaking pass across the screens and the reject stream passes through the screens and is conducted out of the washer through a pipe 16.
  • the screens have slotted openings of about 100 to 300 microns in width.
  • the screens are semi-cylindrical and the slurry is sprayed tangentially onto the screens.
  • Fibers suitable for papermaking pass across the surface of the screens, while small particles, such as kaolin clay, cellulose fines and other suspended solids pass through the screens. Some of the fibers may also pass endwise through the screens.
  • the papermaking fibers from the surface of the screen are included in the accepts stream that is pumped through the pipe 8 and are subject to further cleaning, deinking and processing, indicated at 10, before being supplied through a pipe 12 to a papermaking machine 14.
  • the reject stream from the washer 6 is in the form of a slurry containing less than 1.5% solids.
  • 50% by weight of the solids are fillers such as kaolin clay, calcium carbonate and titanium dioxide.
  • the remaining 50% is mostly sugars, tannins, lignins, and cellulose fiber or fines, which is referred to generally herein as cellulosic material.
  • cellulosic material a material that is referred to generally herein as cellulosic material.
  • This slurry which contains at least 98.5% water, is conducted through the pipe 16 to a dissolved air flotation clarifier 18.
  • Suitable clarifiers are commercially available (e.g., Supracell from Krofta, or Deltafloat from Meri).
  • a flocculating polymer such as Drewfloc 441 from Drew Chemical Co., or Calgon TRP 945, is added to the reject stream in the pipe 16 before the slurry enters the clarifier. Air is injected into the feed stream of the clarifier 18. The slurry fills the clarifier 18, and the flocculated suspended solids float on the air bubbles to the surface of the clarifier. At this point, the mat of solids, which has a consistency of 3 - 9%, is skimmed or raked off the surface and removed from the clarifier through the pipe 20. The clarified water from the clarifier 18 is conducted back into the hydropulper 2 through the pipe 22 to be reused and a portion of the clarified water is recycled via pipe 33 to other places in the mill.
  • a flocculating polymer such as Drewfloc 441 from Drew Chemical Co., or Calgon TRP 945
  • a fiber recovery unit 26 In accordance with this invention, nearly all unscreened mill process effluents that contain papermaking fibers are treated in a fiber recovery unit 26.
  • the stream passes through screens that separate the papermaking fibers from fillers such as kaolin clay, cellulose material, sugars, lignins, tannins, etc., in a manner similar to the washer 6.
  • This effluent includes some reject water streams, dumping or spills from pulp and paper chests, plant wash-ups, etc., indicated as stream 24 in Fig. 1. Previously, this effluent would have been discharged to a sewer.
  • Papermaking fibers are returned through pipe 28 from the fiber recovery unit 26 to the washer 6.
  • Pipe 30 conducts the reject stream from the fiber recovery unit 26 to the clarifier 18.
  • the white water stream 25 from the papermaking machine is supplied to another flotation clarifier 27 where the flocculated suspended solids are removed in the same manner as in the clarifier 18.
  • Process white water stream 23 is returned to the washer 6.
  • the flotate from the clarifiers 18 and 27 is supplied to a heater 36 through pipes 20 and 34 respectively.
  • the heater 36 may be of any suitable type, such as a steam injection unit, or a heat exchanger.
  • the flow rate of the stream and the heat applied should be sufficient to raise the temperature of the stream for sufficient time to achieve pasteurization of the stream.
  • the stream should be heated to a temperature of at least 160° F.
  • the stream passes out of the heat exchanger 36 through a pipe 38, and a second polymer (such as Drewfloc 453 from Drew Chemical Co.) is added to the slurry to cause the solids to dewater as the slurry enters a belt press 40.
  • the belt press can be any one of the commercially available units (e.g., Kompress Belt Filter Press, Model GRS-S-2.0 from Komline Sanderson).
  • the filter cake contains 35-40% solids. Process white water from the belt press is returned to the hydropulper 2 through the pipe 42.
  • a screw press may be used after the belt press, or instead of the belt press.
  • a belt press with compressive rolls can be employed. The filter cake would pass through the nip between the rolls for additional dewatering.
  • the filter cake from the belt press 40 is conveyed by a screw conveyor 44 to a pin mixer 46 (such as the Turbulator from Ferro-Tech).
  • the pin mixer has a cylindrical shell and a rotatable shaft mounted on the central axis of the shell.
  • the shell is stationary and is supported on a frame so that the central axis of the shell is horizontal.
  • the shaft has radial pins that are spaced about 1/8" from the interior wall of the shell.
  • Pieces of the filter cake from the conveyor 44 are deposited in the shell at one end of the shell. The rate of filling of the shell should be adjusted so that the cake material occupies only about 2% of the volume of the shell.
  • the pin mixer 46 By maintaining a low density in the pin mixer 46, the filter cake is broken up by the rotating pins so that individual granules are separated as the material progresses from the inlet of the pin mixer to the outlet. It has been found that the pin mixer 46 produced optimum size particles for use as an agricultural carrier by running in the middle of its speed range, which is at 1500-4500 feet per minute tip speed of pins. Higher speeds give larger particles. Lower speeds yield a larger variability in sizes, with no net increase in smaller sized granules. It has been discovered that, when operating the mixer with a partially filled chamber in the middle of its speed range, the pin mixer 46 reduces the size of the particles as compared to the size of the particles that are discharged from the screw conveyor 44.
  • Fig. 2 The effect of the pin mixer 46 on the particle size is shown in Fig. 2, which compares the percent of particles retained on screens of progressively smaller openings (higher mesh numbers). As shown in Fig. 2, a substantially greater percentage of the particles that are discharged from the pin mixer 46 have a smaller size than the particles entering the pin mixer 46. Another way of stating this is that Fig. 2 shows that only 8% of the particles discharged from the pin mixer 46 have a size large enough to be retained on a #8 mesh screen or larger (e.g., #4), while 25% of the particles supplied to the pin mixer have a size large enough to be retained on a #8 mesh screen or larger.
  • #8 mesh screen or larger e.g., #4
  • Additives may be added at this point (e.g., to increase density or absorbency) but it is important not to increase the water content of the press cake since this would cause the particles to agglomerate, yielding a larger than desirable particle size and a less absorbent product.
  • Operating the pin mixer in this fashion allows for uniform densification of the granules. It has been found that backmixing dried granules with the wet feed prior to the pin mixer also leads to a smaller, denser granule. Preferably, up to 50% by weight of the dried granules can be added.
  • the granulated but still moist material moves, preferably under the force of gravity, onto a swing conveyor 48, to the belt of a conveyor dryer 50, such as a Proctor & Schwartz two-zone conveyor dryer.
  • the belt is porous and a fan blows hot air through the belt to dry the granules.
  • the velocity of the air flow is sufficiently low to avoid movement of the granules on the belt.
  • the granules have a minimum solids content of 90% by weight, and preferably greater than 95%.
  • Vibrating screens 52 such as manufactured by Sweco, are used to classify the material by size according to product specifications.
  • the filter cake from the belt press 40 may be conveyed by a conveyor 54 to a dryer 56, such as a Komline Sanderson paddle-type dryer, as shown schematically in Fig. 1.
  • a dryer 56 such as a Komline Sanderson paddle-type dryer, as shown schematically in Fig. 1.
  • the filter cake particles are further dried and may be ground into fine dry particles.
  • the dried particles may have any desired solids content depending on the time and extent of drying.
  • the particles have a solids content of 90 to 100% by weight. Even more preferably, the particles have a solids content of 96 to 99% by weight.
  • the particles desirably have a bulk density of from 45 lbs/ft 3 to 50 lbs/ft 3 and a size ranging from 4 to 300 mesh.
  • the particles from dryer 56 may be used directly as a product, or optionally mixed with wet filter cake particles at the dry/wet particle mixing stage 60.
  • the dry particles from dryer 56 are conveyed through 62.
  • the wet particles are conveyed through 58.
  • the dried particles from dryer 56 may be returned to the main conveyor 44 and mixed with the filter cake particles to produce a final product.
  • the dry/wet particle mixing whether in a separate mixing stage 60 or in the main conveyor 44 provides a product having a solids content of from 40 to 60% by weight, preferably 45 to 50% by weight.
  • the wet particles from the belt press 40 may be used directly with little or no mixing of dry particles.
  • the particles used as a final product either with or without addition of dry particles from the dryer 56 have a bulk density of from 50 lbs/ft 3 to 60 lbs/ft 3 and a size ranging from 4 to 100 mesh.
  • the mixing ratio of dry particles from dryer 56 to wet particles from belt press 40 ranges from 0 to 50% by weight, preferably 5 to 30% by weight.
  • the purpose of the heater 36 is to prevent the growth of bacteria in the material produced by this process. If the filter cake or the granules from the pin mixer 46 are conducted through a dryer, as described above, the heater 36 may be omitted since any bacteria will be killed in the dryer. However, if coarse wet particles are produced, it is necessary to kill the bacteria.
  • An alternative to the heater 36 would be the use of a stationary horizontal cylinder with a rotating auger that would advance the particles through the cylinder. Steam injected into the cylinder would heat the material sufficiently to cause the bacteria to be killed.
  • the granules produced by this process contain approximately 50% by weight of organic materials, such as cellulosic fines, starches, tannins and lignins.
  • the granules contain less than 10% fiber by weight over 1 mm in length.
  • the inorganic fillers comprise about 50% by weight of the granules and are made up primarily of kaolin clay, calcium carbonate and titanium dioxide.
  • the granules have an irregular, generally spherical shape.
  • the granules from the conveyor dryer 50 vary in size. Typically, about 50% will be retained on an 8 x 16 mesh screen, i.e., 50% would pass through an U.S. Sieve No. 8 mesh screen but would be retained on a 16 mesh screen.
  • the remaining portion would be about 40% in the 16 x 30 mesh size range, and about 10% in the 20 x 60 mesh size range.
  • the granules have a bulk density of about 30-40 lb./cu. ft. Bulk density can be increased by adding prior to the pin mixer a densifier such as Barium Sulfate.
  • the granular material according to the present invention is able to withstand agitation such as might occur during shipment, handling, and storage. Resistance to attrition of the granules is between 90 and 95%. This percentage is based on the following test procedure. A weight of 75 grams of sample is shaken on a limiting screen for ten minutes and 50 grams of the material retained is then shaken in a pan for ten minutes with ten steel balls (5/8" in diameter). The entire sample is then shaken on the limiting screen for ten minutes. The percentage of the original 50 grams retained on the limiting screen is the resistance to attrition cited above. Granular material according to the present invention has been found to generally have a pH between 8.5 - 9.4.
  • Granular material according to the present invention is adapted to absorb various liquids to desired degrees as a function of percentage of weight of the granules.
  • the granular material according to the present invention When the granular material according to the present invention is intended for use as an agricultural carrier, it has a liquid holding capacity (LHC) toward odorless kerosene of between 25-29%.
  • LHC liquid holding capacity
  • the material for use as a floor absorbent when tested with material retained on an 8 x 35 mesh, is able to absorb about 70-80% of its weight of water, and about 50-60% of its weight of oil.
  • the use of the pin mixer is an effective way to obtain smaller particles in an efficient manner. It has also been found that the particles produced using the pin mixer have less tendency to produce dust during the treatment and storage of the dry particles than naturally occurring clay. This is particularly important when the particles are used as an agricultural carrier because of the presence of herbicides or pesticides that may adversely affect workers if substantial amounts of dust are present. These granules are also useful as oil and grease absorbents and as pet litter.

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  • Life Sciences & Earth Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Inorganic Chemistry (AREA)
  • Organic Chemistry (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Mechanical Engineering (AREA)
  • Zoology (AREA)
  • Animal Husbandry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Wood Science & Technology (AREA)
  • Pest Control & Pesticides (AREA)
  • Soil Sciences (AREA)
  • Paper (AREA)
  • Processing Of Solid Wastes (AREA)
  • Separation Of Solids By Using Liquids Or Pneumatic Power (AREA)
  • Cultivation Of Plants (AREA)
EP19990106332 1995-06-07 1996-05-20 Feuchte Grobpartikel und Verfahren zur Herstellung der feuchten Grobpartikel Withdrawn EP0928842A3 (de)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
US47840695A 1995-06-07 1995-06-07
US48284395A 1995-06-07 1995-06-07
US482843 1995-06-07
US478406 1995-06-07
EP19960107993 EP0751253A3 (de) 1995-06-07 1996-05-20 Absorbierendes granuläres Material und Verfahren und Vorrichtung zu dessen Herstellung

Related Parent Applications (1)

Application Number Title Priority Date Filing Date
EP19960107993 Division EP0751253A3 (de) 1995-06-07 1996-05-20 Absorbierendes granuläres Material und Verfahren und Vorrichtung zu dessen Herstellung

Publications (2)

Publication Number Publication Date
EP0928842A2 true EP0928842A2 (de) 1999-07-14
EP0928842A3 EP0928842A3 (de) 2000-04-05

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Family Applications (2)

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EP19960107993 Withdrawn EP0751253A3 (de) 1995-06-07 1996-05-20 Absorbierendes granuläres Material und Verfahren und Vorrichtung zu dessen Herstellung
EP19990106332 Withdrawn EP0928842A3 (de) 1995-06-07 1996-05-20 Feuchte Grobpartikel und Verfahren zur Herstellung der feuchten Grobpartikel

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EP19960107993 Withdrawn EP0751253A3 (de) 1995-06-07 1996-05-20 Absorbierendes granuläres Material und Verfahren und Vorrichtung zu dessen Herstellung

Country Status (7)

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EP (2) EP0751253A3 (de)
JP (1) JP3012196B2 (de)
KR (1) KR970001743A (de)
AR (1) AR002418A1 (de)
AU (1) AU707591B2 (de)
CA (1) CA2176435C (de)
NO (1) NO962375L (de)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2003018504A1 (en) * 2001-08-23 2003-03-06 Kemimäklarna Int. Ab Process for producing a building component or an absorbent product from waste in papermaking
GB2395162A (en) * 2002-09-05 2004-05-19 Salvtech Ltd A method of producing moulded products from waste paper`
WO2006041369A1 (en) 2004-09-10 2006-04-20 Jaernmark Tomas Device and method for production of cellulose-based products
WO2012097938A1 (de) * 2011-01-17 2012-07-26 Voith Patent Gmbh Papiermaschine

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US5622600A (en) * 1993-09-09 1997-04-22 Marcal Paper Mills, Inc. Dyed particulate or granular materials from recycled paper and process for making the materials
US6260511B1 (en) 1996-01-24 2001-07-17 Kimberly-Clark Worldwide, Inc. Process for the preparation of absorbent materials
DE19949265C2 (de) 1999-10-12 2002-09-19 Der Gruene Punkt Duales Syst Verfahren zum Minimieren des Neuwassereinsatzes im Wasserkreislauf bei einer Aufbereitungsanlage
EP3012370B1 (de) * 2014-10-22 2018-08-15 Valmet Technologies, Inc. Klärschlammrecyclingvorrichtung und -verfahren zur Wiederverwendung von Klärschlamm
RU2634235C1 (ru) * 2016-11-11 2017-10-24 Федеральное государственное автономное образовательное учреждение высшего образования "Северный (Арктический) федеральный университет имени М.В. Ломоносова" (САФУ) Способ переработки отходов сортирования сульфатной целлюлозы в формованные изделия
CN109200947A (zh) * 2017-06-29 2019-01-15 高州市恒和新材料有限公司 一种高岭土挤压造粒干燥方法
CN112619872B (zh) * 2020-12-01 2022-11-22 江西都昌金鼎钨钼矿业有限公司 一种磨矿前的预先分级方案

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US4374794A (en) * 1980-05-02 1983-02-22 Kok Cornelis Jacobus M Process for the preparation of a liquid-absorbing and shock-absorbing material
WO1995007384A1 (en) * 1993-09-09 1995-03-16 Marcal Paper Mills, Inc. Process and apparatus for manufacturing absorbent granular material

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US4241001A (en) * 1979-06-22 1980-12-23 J. M. Huber Corporation Process for producing pelletized pigmentary materials
US5248391A (en) * 1992-09-10 1993-09-28 Osa Oil Scavenger Absorbent Oil absorbent material

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US4374794A (en) * 1980-05-02 1983-02-22 Kok Cornelis Jacobus M Process for the preparation of a liquid-absorbing and shock-absorbing material
WO1995007384A1 (en) * 1993-09-09 1995-03-16 Marcal Paper Mills, Inc. Process and apparatus for manufacturing absorbent granular material

Cited By (6)

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CN103328722A (zh) * 2011-01-17 2013-09-25 沃依特专利有限责任公司 造纸机

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JPH09176981A (ja) 1997-07-08
AU5479096A (en) 1996-12-19
NO962375D0 (no) 1996-06-06
EP0751253A3 (de) 1997-11-05
CA2176435C (en) 2002-01-22
NO962375L (no) 1996-12-09
JP3012196B2 (ja) 2000-02-21
CA2176435A1 (en) 1996-12-08
EP0751253A2 (de) 1997-01-02
AU707591B2 (en) 1999-07-15
AR002418A1 (es) 1998-03-11
EP0928842A3 (de) 2000-04-05
KR970001743A (ko) 1997-01-24

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